CN218178620U - Low-temperature liquid adsorber cooling device - Google Patents
Low-temperature liquid adsorber cooling device Download PDFInfo
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- CN218178620U CN218178620U CN202221947125.1U CN202221947125U CN218178620U CN 218178620 U CN218178620 U CN 218178620U CN 202221947125 U CN202221947125 U CN 202221947125U CN 218178620 U CN218178620 U CN 218178620U
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Abstract
The utility model relates to a low temperature liquid adsorber cooling device, the device includes two groups low temperature liquid adsorbers and supporting facility, the device sets up all the way low temperature gas bypass pipeline on the gas product output main line of air separation plant upper tower lower part low temperature gas extraction opening department, carries low temperature product gas cooling adsorber at adsorber regeneration cooling stage, and the low temperature gas after the cooling heat transfer is merged into the gas product output main pipe of heat exchanger cold junction through the output pipeline and is retrieved, adds the low temperature gas cooling system control module of adsorber in air separation plant centralized control system simultaneously and realizes automatic control; the device overcomes various defects that the operation stability of an air separation system is influenced by taking the same medium low-temperature liquid as a cold source, a molecular sieve is easy to break, the low-temperature liquid cannot be recycled after gasification and heat exchange, and the like in the prior art, and has remarkable effects on the operation stability and the economical efficiency of the air separation device.
Description
Technical Field
The utility model belongs to degree of depth refrigeration air separation field, concretely relates to cryogenic liquids adsorber.
Background
The basic principle of deep refrigeration air separation is to condense air into liquid by using a low-temperature rectification method and then separate the air according to the difference of evaporation temperatures of all components.
An air separation plant or unit (air separation plant or unit for short) is mainly composed of the following subsystems: a power system, a purification system, a refrigeration system, a heat exchange system, a rectification system, a product conveying system, a control system and the like; the purification system comprises an air precooling system and a molecular sieve purification system, the precooling system removes physical impurities in the air and simultaneously washes harmful impurities such as acidic substances in the air, and the molecular sieve purification system further removes substances harmful to the operation of the air separation equipment such as water, carbon dioxide, acetylene, propylene, propane, heavy hydrocarbon and nitrous oxide in the air, so that the normal-temperature molecular sieve purification process is widely applied to the air separation industry at home and abroad.
Although the front-end purification system of the air separation device can remove most of the impurities and harmful substances which affect the product purity and the air separation operation, a small amount or trace amount of carbon dioxide, acetylene, hydrocarbon, oxynitride and other harmful impurities enter the rectification system and are retained along with the passage of time, and when the accumulated amount is increased to critical content, the inflammable and explosive substances can bring dangerous safety hazards to the air separation safety; in addition, carbon dioxide, acetylene, hydrocarbon, oxynitride, and the like contained in the air are high boiling point components and mainly accumulate in the low temperature liquid of the rectifying tower. Therefore, a low-temperature liquid adsorber is additionally arranged in the subsequent process of the rectification system of part of air separation equipment, and the function of the low-temperature liquid adsorber is mainly used for further removing carbon dioxide, acetylene, hydrocarbon, oxynitride and other harmful substances dissolved in the low-temperature liquid.
The low-temperature adsorption principle is liquid-phase physical adsorption, and is a reversible adsorption process. The adsorbent in the low-temperature liquid adsorber is porous solid particles, silica gel and molecular sieves are adopted mostly, and the adsorbent can be recycled in a certain period. The adsorption temperature of the silica gel and the molecular sieve in the low-temperature liquid adsorber is lower than-100 ℃, the adsorption capacity of the adsorbent reaches a saturated state when the adsorbent operates to the adsorption capacity transition point, and the adsorption capacity of the silica gel and the molecular sieve in the low-temperature liquid adsorber can be recovered by adopting a heating regeneration method.
Generally, an air separation plant is provided with two low-temperature liquid adsorbers, one of the two low-temperature liquid adsorbers is used for online adsorption, the other low-temperature liquid adsorber is used for regeneration, and the other low-temperature liquid adsorber is used for high-temperature regeneration and normal-temperature standby during regeneration. The method comprises the steps of setting the adsorption time of a low-temperature liquid adsorber by calculating the periodic value of the adsorption capacity transition point of an adsorbent, switching one low-temperature liquid adsorber which is in a normal-temperature standby state after regeneration into a low-temperature online adsorption state by switching when the online adsorption time of 1 low-temperature liquid adsorber reaches the set time, and simultaneously switching the other low-temperature liquid adsorber which reaches the online adsorption time into a regeneration standby state.
The regeneration standby process of the low-temperature liquid adsorber comprises six stages of liquid drainage, standing, blowing, heating, cold blowing and normal-temperature standby, and the switching operation process of the low-temperature liquid adsorber comprises four stages of cooling, liquid injection, parallel connection and adsorption operation. In the prior art, in the cooling stage of the switching process of the low-temperature liquid adsorber, the low-temperature liquid of a product is widely used as a cold source for cooling the low-temperature liquid adsorber, and when the low-temperature liquid adsorber is cooled to the working temperature of the low-temperature liquid, the low-temperature liquid adsorber is switched to a low-temperature liquid injection state from a normal-temperature standby state to be ready for operation.
At present, in domestic and foreign air separation devices, the process of using low-temperature liquid as a cold source of a low-temperature liquid adsorber in the cooling stage of the switching process of the low-temperature liquid adsorber has the following disadvantages.
The first problem is that: the working condition of the air separation device is influenced.
The low-temperature liquid entering the low-temperature liquid adsorber cools the low-temperature liquid adsorber, is regulated by the liquid discharge valve and is discharged to the atmosphere, the low-temperature liquid cannot be recycled, and the low-temperature liquid has large influence on the balance of system cold quantity material components, the operation working condition and the equipment stability of the air separation device, the operation safety of the low-temperature liquid adsorber and the full-period use time.
The low-temperature liquid absorber is used for cooling the low-temperature liquid in a normal-temperature standby state, the low-temperature liquid is vaporized by heat, the vaporization amount is large, and the low-temperature liquid is discharged to the atmosphere after vaporization heat exchange, so that the loss of the low-temperature liquid is high, and the cold quantity and the material loss of an air separation system are large. In order to maintain the balance between the refrigerating capacity of the air separation system and the lost refrigerating capacity of the system, the refrigerating capacity of the equipment system needs to be increased, the output of low-temperature liquid products needs to be reduced, and the running cost of the equipment is increased. The low-temperature liquid cools the low-temperature liquid absorber and is discharged to the atmosphere, so that the low-temperature liquid absorber cannot be recycled, the balance of materials and components of the low-temperature rectifying tower is influenced, the purity of gas and liquid products is reduced, the purity of the gas and liquid products of equipment is maintained, and the yield of the gas products is reduced. The low-temperature liquid cools the low-temperature liquid absorber and discharges the atmosphere, and the balance working condition of the equipment cold quantity, the materials and the components fluctuates, so that the actual operation working condition of the low-temperature rectifying tower deviates from the designed operation working condition.
The second problem is that: affecting the safe and stable operation of the air separation device.
The low-temperature liquid cools the low-temperature liquid absorber and is discharged to the atmosphere, the loss of the low-temperature liquid is high in a short time, and the liquid level of the low-temperature liquid in the rectifying tower and the heat exchanger is low, so that the stable operation of equipment is endangered. The low-temperature liquid enters the low-temperature liquid adsorber for cooling, the vaporization amount of the low-temperature liquid is large in a short time, and the pressure of the low-temperature liquid adsorber is high, so that the safe operation of equipment is endangered.
The third problem is that: affecting the service life of the molecular sieve.
The low-temperature liquid is cooled and instantly gasified in a low-temperature liquid adsorber, the temperature of the low-temperature liquid adsorber is greatly reduced in a short time, the breakage rate of silica gel and molecular sieves in the adsorber is high, and the full-period service time of the low-temperature liquid adsorber is short. Most of low-temperature adsorption molecular sieves are imported and have higher price, the breaking rate of the molecular sieves is high, and the running cost of equipment is increased.
The fourth problem is that: the workload of manual operation is increased.
The low-temperature liquid enters the low-temperature liquid adsorber for cooling, the fluctuation of the operation condition of the equipment is large in a short time and exceeds the automatic adjustment range of the equipment, manual intervention and adjustment are necessary, and the operation load of the equipment is large.
35000m designed and manufactured by French air separation liquefaction company 3 The/h oxygen external compression flow air separation device is taken as an example and is explained by combining the figure 1:
35000m 3 the air separation plant is provided with 2 liquid oxygen adsorbers, the adsorbent is a 5A molecular sieve, and 1 air separation plant performs online adsorption and 1 air separation plant performs regeneration for standby. The liquid oxygen adsorption temperature of the liquid oxygen adsorber is minus 180 ℃, the regeneration heating temperature of the liquid oxygen adsorber is 100 ℃, and the standby temperature is 20 ℃. In the cooling stage of the liquid oxygen absorber switching process, liquid oxygen at-180 ℃ is designed to be used as a cold source for cooling the liquid oxygen absorber, the liquid oxygen at-180 ℃ in a liquid inlet pipeline of the liquid oxygen absorber adsorbed on line is injected into a standby liquid oxygen absorber at the temperature of 20 ℃, the standby liquid oxygen absorber is cooled, then the standby liquid oxygen absorber is adjusted to discharge atmosphere through a liquid discharge valve, and when the temperature of an outlet of the standby liquid oxygen absorber is reduced to-180 ℃, the liquid oxygen absorber is cooled.
35000m 3 The design of the liquid oxygen absorber of the/h air separation plant is 1 cooling liquid injection regulating valve which is specially used for cooling and liquid injection functions of the liquid oxygen absorber. And in the cooling stage of the switching process of the liquid oxygen adsorber, opening a cooling liquid injection regulating valve and a liquid discharge valve, and when liquid oxygen is injected into the standby adsorber, the liquid oxygen loss is more than 10.82m3/h, and the liquid oxygen level of the main cold evaporation side is reduced to a low alarm value of 60% from a design operation value of 80%.
In order to avoid the liquid oxygen level at the main cooling evaporation side from reducing to 50 percent of an interlocking value to cause 35000m 3 Stopping the production of liquid oxygen and liquid nitrogen products and reducing the yield of liquid argon to reduce the liquid oxygen liquid level amplitude reduction of a main cold evaporation side in the cooling stage of the switching process of the liquid oxygen absorber; at the same time, 35000m is increased 3 The expansion amount of an expansion machine of the air separation plant is increased, the refrigerating capacity of the plant is increased, the liquid oxygen level of a main cold evaporation side is larger than the interlocking value of the main cold evaporation side, the purity of nitrogen extracted by a rectifying tower is reduced, and the nitrogen yield is reduced to 35000m to ensure that the nitrogen purity reaches the design value 3 The nitrogen yield of the air separation device is less than the design value; in addition, the liquid oxygen level on the main cold evaporation side is not smallAt the low alarm value, the liquid oxygen flow at the outlet end of the liquid oxygen adsorber in the on-line adsorption state is reduced, resulting in 35000m 3 The oxygen output of the air separation plant is less than the design value.
At opening 35000m 3 And h, cooling the liquid oxygen absorber of the air separation plant by using a liquid injection regulating valve and a liquid discharge valve, wherein when liquid oxygen is injected into the standby liquid oxygen absorber, the liquid oxygen is instantaneously vaporized, and the pressure of the standby liquid oxygen absorber is increased to a high alarm value of 1MPa. In order to avoid the pressure of the standby liquid oxygen absorber rising to an interlocking value of 1.5MPa, the whole system is automatically stopped, the opening degree of a liquid discharge valve of the liquid oxygen absorber is increased, the pressure of the liquid oxygen absorber is reduced, the liquid oxygen discharge capacity of the standby liquid oxygen absorber is increased, and the liquid oxygen liquid level and the oxygen output of the main cold evaporation side are reduced again.
At 35000m 3 In the cooling stage of the switching process of the liquid oxygen adsorber of the air separation plant, the standby liquid oxygen adsorber is cooled to minus 180 ℃ from the standby temperature of 20 ℃ for 1 hour, the breaking rate of the molecular sieve is high, the replacement time of the 5A molecular sieve designed by French air separation liquefaction company is less than 8 years, and the service cycle is short.
At 35000m 3 And (3) within 1 hour of cooling the liquid oxygen adsorber of the air separation plant, the working conditions of the expansion machine, the heat exchanger, the lower tower, the main cooling tower, the upper tower, the crude argon tower and the fine argon tower must be synchronously adjusted, so that the stable operation working condition of the air separation plant can be kept.
SUMMERY OF THE UTILITY MODEL
Technical problem to be solved
The defect that exists to prior art, the utility model provides a low temperature liquid adsorber cooling device has solved a series of problems that the low temperature liquid short time internal loss volume of regard as the cold source brought greatly among the prior art, including causing equipment operation operating mode undulant great, endanger equipment steady operation and adsorber in silica gel, the high scheduling problem of molecular sieve percentage of damage.
(II) technical scheme
In order to achieve the above purpose, the utility model discloses a following technical scheme realizes: a cooling device for a low-temperature liquid adsorber.
The utility model relates to a low temperature liquid adsorber (hereinafter referred to as adsorber) cooling device, technology includes two sets of adsorber systems, and one is used for one and is equipped with, switches process cooling stage at the adsorber, and the low temperature gas that produces after air separation by air separation passes through the pipeline as the cold source of adsorber and gets into the adsorber, cools off the adsorber under the normal atmospheric temperature standby state, falls to operating temperature until the adsorber temperature, and the adsorber changes over to low temperature liquid by the normal atmospheric temperature standby state and annotates the liquid state to carry out recycle to the low temperature gas that goes out the adsorber.
The utility model discloses the device specifically does: a low-temperature liquid adsorber cooling device comprises two groups of low-temperature liquid adsorbers and supporting facilities thereof, wherein the low-temperature liquid inlet header pipe is connected with a main cold taking port of a rectifying tower of an air separation plant, the liquid inlet header pipe is divided into two liquid inlet branch pipes which are connected in parallel, each liquid inlet branch pipe is respectively provided with a liquid inlet valve, a group of adsorbers are respectively connected behind each liquid inlet valve, a liquid outlet pipeline is respectively arranged behind each group of adsorbers, the two liquid outlet pipelines are connected in parallel, each liquid outlet pipeline is respectively provided with an outlet valve, each liquid outlet pipeline in front of the outlet valve is respectively provided with a liquid outlet pipeline, each liquid outlet pipeline is respectively provided with a liquid outlet valve, and the two liquid outlet pipelines are gathered into a liquid outlet header pipe behind the liquid outlet valves and connected to the rectifying tower of the air separation plant; the method is characterized in that: the method comprises the following steps that a low-temperature gas bypass pipeline is arranged on a gas product output main pipeline at a low-temperature gas taking port at the lower part of an upper tower of the air separation equipment and is used as a low-temperature gas inlet main pipe for cooling an adsorber, the low-temperature gas inlet main pipe is divided into two low-temperature gas inlet branch pipes which are respectively connected to the two low-temperature gas inlet branch pipes behind a liquid inlet valve and in front of the adsorber of the existing equipment, a pneumatic air inlet regulating valve is respectively arranged on each of the two low-temperature gas inlet branch pipes, and the two pneumatic air inlet regulating valves are arranged in parallel and respectively control and regulate the low-temperature gas inlet flow entering the two sets of adsorbers; meanwhile, two outlet branch pipes are respectively arranged on two outlet pipelines behind the absorber and in front of the liquid discharge valve and the outlet valve, a pneumatic outlet regulating valve is respectively arranged on the two outlet branch pipes, and the two pneumatic outlet regulating valves are arranged in parallel and respectively control and regulate the pressure of the two outlet branch pipes; and one low-temperature gas outlet header pipe of the two gas outlet branch pipe assemblies behind the pneumatic outlet regulating valve is connected to a gas product outlet header pipe at the front cold end of the main heat exchanger, and the collected product gas is reheated to normal temperature through the heat exchanger and is input into a compressor or a gas pipe network.
The utility model discloses further technical scheme does: and a flowmeter is arranged on the low-temperature gas inlet main pipe, the flowmeter is arranged in front of the pneumatic inlet regulating valves on the two gas inlet branch pipes, a pressure transmitter and a thermometer are sequentially arranged on the low-temperature gas outlet main pipe, and the transmitter and the thermometer are arranged behind the pneumatic outlet regulating valves on the two gas outlet branch pipes.
The material and pressure grade of the low-temperature gas inlet main pipe are the same as those of the gas product output main pipe, and the diameter of the low-temperature gas inlet main pipe is calculated according to the low-temperature gas design flow value of the adsorber.
For realizing the above device automation control, the utility model discloses the device is technical scheme further does: the method is characterized in that a low-temperature gas cooling system control module of an adsorber is additionally arranged in a centralized control system of the air separation device, the gas flow in a low-temperature gas inlet pipeline, the gas pressure in a gas outlet pipeline and a gas temperature interlocking value are set in the cooling system control module, and a pneumatic gas inlet regulating valve, an outlet regulating valve switch and the opening of a valve are automatically controlled and regulated.
And in the cooling stage of the adsorber, the automatic control switch of the low-temperature gas cooling system is put into operation, the pneumatic air inlet regulating valve and the pneumatic outlet regulating valve are automatically opened, the opening of the valve is automatically regulated according to the set values of the flowmeter and the thermometer, and the flow of the low-temperature gas entering the adsorber and the pressure of the low-temperature liquid adsorber are automatically regulated.
Adding a low-temperature gas inlet pipeline flow and outlet pipeline pressure interlocking value in a DCS or PLC control system of the air separation plant, and when the low-temperature gas inlet pipeline flow and the outlet pipeline pressure value rise to the interlocking values, automatically and fully closing a pneumatic inlet regulating valve and automatically and fully opening a pneumatic outlet regulating valve; meanwhile, a temperature interlocking value is additionally arranged in a DCS or PLC control system of the air separation plant, when the temperature of a low-temperature gas outlet pipeline is reduced to a low interlocking value, a pneumatic air inlet adjusting valve and a pneumatic outlet adjusting valve are automatically closed, and the cooling process of the absorber is finished; meanwhile, the liquid injection valve of the absorber is automatically opened, and the low-temperature liquid absorber enters a liquid injection stage.
(III) advantageous effects
The utility model provides a cooling device of cryogenic liquids adsorber possesses following beneficial effect:
1. at first, the utility model discloses an use low-temperature gas to replace cryogenic liquid as cold source cooling adsorber, solved cryogenic liquid adsorber and switched process cooling stage, the high problem of cryogenic liquid loss volume.
2. Secondly, the utility model discloses technical scheme more does benefit to and keeps air separation plant material, component, cold volume balance, is favorable to maintaining air separation plant safety, stable, economic operation.
3. Furthermore, the utility model discloses the device adds the low temperature gas cooling system control module of adsorber in air separation plant DCS or PLC centralized control system, sets up air inlet regulating valve, export governing valve into pneumatic valve simultaneously, realizes the full automatic operation of cryogenic liquids adsorber.
Drawings
FIG. 1 is a schematic diagram of a prior art air separation plant liquid oxygen adsorber cooling process;
FIG. 2 is a schematic view of a cooling process of a liquid oxygen adsorber of an oxygen external compression process air separation plant according to an embodiment of the present invention;
FIG. 3 is a schematic view of a control system according to an embodiment of the present invention;
description of the figures the symbols: c1, discharging from the tower; c2, main condensation evaporator (main cooling); c3, feeding into a tower; c4, an oxygen compressor; b1, a liquid oxygen adsorber 1; b2, a liquid oxygen adsorber 2; e2, a main heat exchanger; l1, an oxygen product output header pipe; l2, a low-temperature oxygen inlet main pipe; l3, a low-temperature oxygen outlet header pipe; l21 and B1 low-temperature gas inlet branch pipes; l22 and B2 low-temperature gas inlet branch pipes; l31 and B1 low-temperature gas outlet branch pipes; l32 and B2 low-temperature gas outlet branch pipes; v1 and B1 liquid inlet valves; v3, B1 outlet valves; v2 and B2 liquid inlet valves; v4, B2 outlet valves; v7, a liquid oxygen absorber cooling liquid injection valve; v5 and B1 pneumatic air inlet adjusting valves; v6 and B2 pneumatic air inlet adjusting valves; v8, B1 pneumatic outlet regulating valves; v9, B2 pneumatic outlet regulating valves; v10 and B1 drain valves; v11 and B2 drain valves; f1, a flow meter; p1, a pressure transmitter; t1, a thermometer.
Detailed Description
The embodiments of the technical solution of the present invention are clearly and completely described below with reference to fig. 2 and fig. 3. The embodiment described below is only one embodiment of the technical solution of the present invention, and not all embodiments.
The embodiment of the utility model provides a: oxygen external compression process 35000m 3 A cooling device of a liquid oxygen adsorber of an air separation plant.
At 35000m 3 In the process flow design of the air separation equipment, the parameters of the product oxygen extracted from a low-temperature gas taking port at the lower part of an upper tower C3 of a rectifying tower of the air separation equipment are as follows: the temperature is-181.5 ℃, the pressure is 45KPa, the purity is 99.6 percent, and the parameters of the liquid oxygen extracted from the bottom of the main cooling C2 and entering the liquid oxygen adsorbers B1 and B2 are as follows: the temperature is-180 ℃, the pressure is 70KPa, and the purity is 99.6 percent; the temperature of the product oxygen is 1.5 ℃ lower than that of the liquid oxygen, and the product oxygen can cool the liquid oxygen absorber B1/B2 to a temperature lower than minus 180 ℃ through design and calculation.
For this purpose, at 35000m 3 In the design of the process flow of the air separation equipment, in the cooling stage of the switching process of the liquid oxygen absorber B1 or B2, product oxygen is designed to be used as a cold source of the cooling liquid oxygen absorber B1 or B2.
In the prior art, the design flow of the liquid oxygen cooling liquid oxygen adsorber is F =17.3m 3 Liquid state, cooling time 1 hour, liquid oxygen density ρ 1=1140kg/m 3 Liquid oxygen vaporization latent heat r =6816j/mol, oxygen specific volume c =0.91 j/(g.k), and oxygen density ρ 2=1.284kg/m after liquid oxygen vaporization 3 Volume V1=17.3m of liquid oxygen adsorber 3 Temperature drop of a liquid oxygen cooling liquid oxygen adsorber Δ t1=20- (-180 ℃) =200 ℃, cold release quantity of the liquid oxygen cooling liquid oxygen adsorber Q1= (V1 × ρ 1/32) × r + c × ρ 2 × V1 × Δ t1=8240423.1KJ, temperature drop of a product oxygen cooling liquid oxygen adsorber Δ t2=20- (-181.5 ℃) =201.5 ℃, cold release quantity Q2= c × ρ 2 × V2 × Δ t2, and Q1= Q2 is set to derive total product oxygen cooling liquid oxygen adsorberVolume V2= Q1/c × ρ 2 × Δ t2, about 35000m 3 。
According to the physical properties of the 5A molecular sieve adsorbent, the cooling rate is 20 ℃/h, the 5A molecular sieve has low breakage rate, so the cooling rate of the product gas oxygen cooling liquid oxygen adsorber is controlled to be 20 ℃/h per hour, and when the product gas oxygen cooling liquid oxygen adsorber is cooled to the working temperature of-180 ℃, the temperature is cooled for 10 hours at 200 ℃.
Therefore, the total volume of the oxygen absorber required for one time by adopting the product oxygen cooling liquid is about 35000m 3 The uniform cooling at 200 ℃ needs 10 hours, and the average flow per hour is about 3500m 3 /h。
In order to implement the technical scheme, the low-temperature liquid adsorber and the supporting facilities thereof are improved on the basis of the existing low-temperature liquid adsorber, the device in the prior art comprises two groups of low-temperature liquid adsorbers and supporting facilities thereof, wherein the low-temperature liquid adsorber comprises a liquid oxygen inlet main pipe connected with a main cold C2 material taking port of an air separation plant rectifying tower, the liquid inlet main pipe is divided into two liquid inlet branch pipes, the two liquid inlet branch pipes are connected in parallel, each liquid inlet branch pipe is respectively provided with a liquid inlet valve, the liquid oxygen adsorber B1 is connected with the liquid oxygen adsorber V1 after the liquid inlet valve V2, the liquid oxygen adsorber B2 is connected with the liquid oxygen valve after the liquid inlet valve V2, the two liquid outlet pipes are respectively arranged after the liquid oxygen adsorber B1 or B2, the two liquid outlet pipes are connected in parallel, the liquid outlet valve V3 is arranged on the liquid oxygen adsorber B1, a liquid discharge pipe is arranged before the liquid oxygen adsorber V3, a liquid discharge valve V10 is arranged on the liquid discharge pipe, an outlet valve V4 is arranged on the liquid oxygen adsorber B2, a liquid discharge pipe is arranged before the liquid oxygen adsorber V4, a liquid discharge pipe is arranged on the liquid discharge pipe, a liquid discharge valve V11 is arranged on the liquid discharge pipe, and the two liquid discharge pipe are gathered into a liquid discharge pipe and connected to the rectifying tower, and return to the air separation plant rectifying tower, and the air separation plant rectifying plant. In the prior art, in the cooling stage of the switching process of the liquid oxygen adsorber, the adsorber in the regeneration process needs to be cooled by adopting product liquid oxygen, so that a cooling liquid injection pipeline is arranged between two liquid inlet branch pipes which are connected in parallel and are arranged in front of the adsorbers B1 and B2 after the liquid inlet valves V1 and V2, a cooling liquid injection valve V7 is arranged on the liquid injection pipeline, when one group of adsorbers are in the cooling stage of the regeneration process, the V7 is opened to inject the product liquid oxygen to cool the adsorbers, the liquid outlet valve V3 or V4 matched with the regeneration adsorber is closed at the moment, the liquid outlet valve V10 or V11 is opened, and the liquid oxygen (including vaporized oxygen) after cooling and heat exchange is discharged into the atmosphere through the liquid outlet valve.
The utility model discloses the device sets up low temperature oxygen by-pass line of the same kind on the oxygen product output main line L1 of the gaseous extraction mouth department of lower part low temperature of upper tower C3 of air separation plant, as the low temperature oxygen inlet manifold L2 that the cooling adsorber used, low temperature oxygen inlet manifold L2 divide into two way air intake branch pipe and insert respectively before low temperature oxygen adsorber B1 and B2, liquid oxygen adsorber B1 low temperature oxygen inlet branch pipe L21 is connected to the liquid intake branch pipe of the same kind behind current equipment feed liquor valve V1, before adsorber B1, liquid oxygen adsorber B2 low temperature oxygen inlet branch pipe L22 is connected to the liquid intake branch pipe of the same kind behind current equipment feed liquor valve V2, before adsorber B2, respectively install a pneumatic air admission governing valve V5 and V6 on two way low temperature oxygen inlet branch pipe L21 and L22; meanwhile, a low-temperature oxygen outlet branch pipe L31 is arranged on a liquid outlet pipeline behind the liquid oxygen absorber B1 and in front of the liquid discharge valve V10 and the outlet valve V3, a low-temperature oxygen outlet branch pipe L32 is arranged on a liquid outlet pipeline behind the liquid oxygen absorber B2 and in front of the liquid discharge valve V11 and the outlet valve V4, a pneumatic outlet adjusting valve V8 and a pneumatic outlet adjusting valve V9 are respectively arranged on the two gas outlet branch pipes L31 and L32, the two gas outlet branch pipes L31 and L32 which are connected in parallel are gathered into a low-temperature oxygen outlet header pipe L3 after the pneumatic outlet adjusting valves V8 and V9, the pipe L3 is connected with an oxygen product outlet header pipe L1 before the main heat exchanger, and the cooled low-temperature oxygen is recycled.
The air inlet regulating valves V5 and V6 and the outlet regulating valves V8 and V9 adopt DN100 low-temperature pneumatic film regulating valves, and the oxygen flow and the pressure of the bypass low-temperature product are accurately regulated.
A flowmeter F1 is arranged on the low-temperature oxygen inlet main pipe L2, the flowmeter F1 adopts a power bar flowmeter, and the measurement precision is high and the resistance is low; a pressure transmitter P1 and a thermometer T1 are sequentially arranged on the low-temperature oxygen outlet manifold L3, and the thermal resistance thermometer T1 adopts a platinum resistance thermometer and is suitable for a low-temperature environment with the lower limit of-200 ℃; pressure transmitter P1 adopts intelligent differential pressure transmitter, and measurement accuracy is high, is fit for automatic control and adjusts pneumatic valve.
The working flow of the device of the embodiment is as follows: in the regeneration cooling stage of the liquid oxygen adsorber B1 or B2, a pneumatic air inlet adjusting valve V5 or V6 is opened, low-temperature product oxygen is led out from an oxygen product output main pipeline L1 at a material taking port at the lower part of an upper tower C3, is conveyed to a branch pipe L21 or L22 through a bypass low-temperature oxygen inlet main pipe L2, enters the low-temperature liquid adsorber B1 or B2, is cooled through heat exchange with a filler in the adsorber, is discharged through a low-temperature oxygen outlet branch pipe L31 or L32, is adjusted through an outlet adjusting valve V8 or V9, is gathered to a low-temperature oxygen outlet main pipe L3 and is pumped out, is merged into a low-temperature product oxygen main pipe L1 at the cold end of a main heat exchanger E2, is reheated to the normal temperature through the main heat exchanger E2, is led into an oxygen compressor C4 for compression, and is input into an oxygen pipe network.
In this embodiment, the bypass low-temperature oxygen inlet header pipe L2 and the branch pipes L21 or L22, and the low-temperature oxygen outlet header pipe L3 and the branch pipes L31 or L32 are all the same as the diameters of the liquid inlet pipe and the liquid outlet pipe of the low-temperature liquid adsorber B1/B2 of the original equipment, and are all 0.1m, made of aluminum alloy, and have a pressure rating of 2.5MPa.
The diameter D =0.3m of the oxygen product outlet manifold L1 in this example, the length L =22m of the tubes from the lower part of the upper column C3 to the cold end of the main heat exchanger E2, the oxygen density ρ =1.39kg/m3, and the oxygen viscosity μ =2.05 × 10 "5 kg/m.s. When the liquid oxygen absorber B1 or B2 is cooled, the product oxygen flow F =31500m 3 And/h, the initial inlet pressure of the product oxygen pipeline L1 is P =45KPa, and the resistance hf of the product oxygen pipeline L1 from the lower part of the upper tower C3 to the cold end of the main heat exchanger E2 is calculated by Re =4 Fp/3.14 Dmu, lambda =64/Re, hf = lambda x L/D x rho V2/2= lambda x L/D x rho x (4F/3.14D2) 2/2, thereby obtaining that the inlet pressure of the product oxygen output main pipeline at the cold end of the main heat exchanger E2 is P =45-hf =45-1.1KPa =43.9 KPa.
In this embodiment, the diameters of the low-temperature oxygen inlet header pipe L2 and the branch pipe L21 or L22 for cooling are both D =0.1m, and low-temperature oxygen enters and cools the liquid oxygen adsorber B1 or B2 through the inlet header pipe L2 and the branch pipe L21 or L22, is discharged from the low-temperature oxygen outlet branch pipe L31 or L32, flows through the low-temperature oxygen outlet header pipe L3, and is merged into oxygenThe gaseous product exits the cold end of main heat exchanger E2 in header L1 during which the total length L =25m of cryogenic oxygen passing tubes. Low temperature oxygen inlet flow rate F =3500m for coolant oxygen adsorber B1 or B2 3 And/h, initial intake pressure P =45KPa, and by Re =4F ρ/3.14D μ, λ =64/Re, hf = λ × L/D × ρ × V2/2= λ × L/D × ρ × (4F/3.14d 2) 2/2, resistance hf =0.8KPa to the low-temperature oxygen, that is, intake pressure P =45-hf =45-0.8kpa =44.2kpa after the low-temperature oxygen is discharged from the adsorber and enters the cold end of main heat exchanger E2, is calculated.
Therefore, the inlet pressure P =44.2KPa at the cold end of the main heat exchanger E2 after the low-temperature oxygen is discharged from the adsorber, and is 43.9KPa higher than the inlet pressure at the cold end of the main heat exchanger E2 of the oxygen product output header L1, so that the low-temperature oxygen entering the adsorber can be smoothly discharged and merged into the cold end of the main heat exchanger E2 of the oxygen product output header L1 under the action of pressure difference after being cooled, and the low-temperature oxygen can be completely recycled after being cooled.
At 35000m 3 In a DCS control system of an/h air separation plant, a bypass low-temperature oxygen cooling liquid oxygen adsorber B1 or B2 automatic control logic module of a cooling adsorber is additionally arranged, and the low-temperature oxygen flow set value is designed to be 3500m 3 The pressure set values are respectively 44KPa, and the opening degrees of a pneumatic type air inlet regulating valve V5 or V6 and a pneumatic type outlet regulating valve V8 or V9 are automatically adjusted according to the low-temperature oxygen flow and the pressure set values, so that the working flow and the pressure of the bypass low-temperature oxygen are respectively 3500m under automatic control 3 H, 44KPa; the interlock value of the bypass low-temperature oxygen inlet flow is 4500m 3 The interlocking value of the outlet pressure of the B1 or B2 of the liquid oxygen absorber is 50KPa, and the flow value of the low-temperature oxygen inlet main pipe L2 and the pressure value of the gas outlet main pipe L3 are increased to the interlocking value of 4500m 3 When the pressure is/h and 50KPa, the pneumatic air inlet adjusting valve V5 or V6 is automatically and fully closed, and the pneumatic outlet adjusting valve V8 or V9 is automatically and fully opened; the temperature interlocking value of the bypass low-temperature oxygen outlet is designed to be-180.5 ℃, and when the temperature of the bypass low-temperature oxygen outlet main pipe is reduced to-180.5 ℃, the pneumatic air inlet adjusting valve V5 or V6 and the pneumatic outlet adjusting valve V8 or V9 are automatically and completely closed.
This embodiment 35000m 3 Per oxygen external compression process air separation equipmentThe full-automatic operation method of the liquid oxygen absorber B1 or B2 low-temperature product oxygen cooling device is as follows:
when the liquid oxygen absorber B1 is in a normal-temperature standby state and the liquid oxygen absorber B2 is in an online adsorption state, the liquid oxygen absorber B1 is kept in a fully-closed state by a liquid inlet valve V1, an outlet valve V3, a liquid injection valve V7, a liquid discharge valve V10, a pneumatic air inlet regulating valve V5 and an outlet regulating valve V8; and (3) keeping the liquid inlet valve V2 and the outlet valve V4 of the liquid oxygen adsorber B2 in a fully open state, and keeping the pneumatic air inlet regulating valve V6, the pneumatic outlet regulating valve V9 and the pneumatic liquid outlet valve V11 in a fully closed state.
When the liquid oxygen adsorber B1 is in the regeneration cooling stage, the opening is automatically controlled, the pneumatic air inlet adjusting valve V5 and the pneumatic outlet adjusting valve V8 of the liquid oxygen adsorber B1 are automatically opened, the valve openings of the pneumatic air inlet adjusting valve V5 and the pneumatic outlet adjusting valve V8 are automatically adjusted, and the bypass low-temperature oxygen flow is adjusted to 3500m 3 Controlling the pressure of a bypass low-temperature oxygen outlet not to be lower than 44KPa, and controlling a cooling liquid oxygen absorber B1; when the temperature value displayed by a thermometer T1 on the low-temperature oxygen outlet header pipe L3 is reduced to minus 180.5 ℃, the pneumatic air inlet regulating valve V5 and the pneumatic outlet regulating valve V8 are automatically closed, and the cooling of the liquid oxygen absorber B1 is finished; and opening the liquid injection valve V7, injecting liquid oxygen into the liquid oxygen adsorber B1, putting the liquid oxygen adsorber B1 into an online adsorption state, and switching the liquid oxygen adsorber B2 to enter a regeneration process.
Oxygen external compression flow 35000m set in iron and steel industry 3 The method is characterized in that a liquid oxygen absorber of the air separation plant is cooled by low-temperature oxygen, the pressure of the liquid oxygen absorber is maintained at 44KPa without fluctuation in the process of regenerative cooling, the cooling finishing temperature of the liquid oxygen absorber is-180.5 ℃, the cooling time is 10 hours, the working conditions of a rectifying tower and a crude argon tower of the air separation plant are both in a design area, the whole air separation plant runs stably, and the working conditions are not fluctuated obviously.
In summary, the process and the apparatus of this embodiment can be implemented based on the technical solution of the present invention, and the connection mode, the valve and the meter configuration of the apparatus can be replaced arbitrarily; the utility model discloses the low temperature gas that indicates can be low temperature oxygen or any other work media that are suitable for the technical scheme of the utility model.
Although the embodiment of the utility model provides a be applied to steel industry air separation plant, but also be applicable to chemical industry air separation plant low temperature liquid adsorber cooling device simultaneously.
All references to the above cases are within the scope of this patent.
Claims (3)
1. A low-temperature liquid adsorber cooling device comprises two groups of low-temperature liquid adsorbers and supporting facilities thereof, wherein the low-temperature liquid inlet header pipe is connected with a main cold taking port of a rectifying tower of an air separation plant, the liquid inlet header pipe is divided into two liquid inlet branch pipes which are connected in parallel, each liquid inlet branch pipe is respectively provided with a liquid inlet valve, a group of adsorbers are respectively connected behind each liquid inlet valve, a liquid outlet pipeline is respectively arranged behind each group of adsorbers, the two liquid outlet pipelines are connected in parallel, each liquid outlet pipeline is respectively provided with an outlet valve, each liquid outlet pipeline in front of the outlet valve is respectively provided with a liquid outlet pipeline, each liquid outlet pipeline is respectively provided with a liquid outlet valve, and the two liquid outlet pipelines are gathered into a liquid outlet header pipe behind the liquid outlet valves and connected to the rectifying tower of the air separation plant; the method is characterized in that: the method comprises the following steps that a low-temperature gas bypass pipeline is arranged on a gas product output main pipeline at a low-temperature gas taking port at the lower part of an upper tower of the air separation equipment and is used as a low-temperature gas inlet main pipe for cooling an adsorber, the low-temperature gas inlet main pipe is divided into two low-temperature gas inlet branch pipes which are respectively connected to the two liquid inlet branch pipes behind a liquid inlet valve and in front of the adsorber of the existing equipment, and a pneumatic air inlet adjusting valve is respectively arranged on each of the two liquid inlet branch pipes; and simultaneously, two outlet branch pipes are respectively arranged on two outlet pipelines behind the absorber and in front of the liquid discharge valve and the outlet valve, a pneumatic outlet regulating valve is respectively arranged on the two outlet branch pipes, and one low-temperature gas outlet main pipe of the two outlet branch pipe assembly behind the pneumatic outlet regulating valve is connected to a gas product output main pipe in front of the main heat exchanger.
2. The cryogenic liquid adsorber cooling device of claim 1 wherein: and a flowmeter is arranged on the low-temperature gas inlet main pipe, the flowmeter is arranged in front of the pneumatic inlet regulating valves on the two gas inlet branch pipes, a pressure transmitter and a thermometer are sequentially arranged on the low-temperature gas outlet main pipe, and the transmitter and the thermometer are arranged behind the pneumatic outlet regulating valves on the two gas outlet branch pipes.
3. The cryogenic liquid adsorber cooling device of claim 2 wherein: the air separation device centralized control system is additionally provided with a low-temperature gas cooling system control module of an adsorber, the cooling system control module is used for setting the gas flow in a low-temperature gas inlet main pipe, the gas pressure in a low-temperature gas outlet main pipe and a gas temperature interlocking value, and the pneumatic inlet regulating valve, the pneumatic outlet regulating valve switch and the valve opening are automatically controlled and regulated.
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| CN115265092A (en) * | 2022-07-27 | 2022-11-01 | 安徽马钢气体科技有限公司 | Low-temperature liquid adsorber cooling process and device |
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