CN114307866A - Novel reaction system of propane dehydrogenation device - Google Patents
Novel reaction system of propane dehydrogenation device Download PDFInfo
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- CN114307866A CN114307866A CN202111001309.9A CN202111001309A CN114307866A CN 114307866 A CN114307866 A CN 114307866A CN 202111001309 A CN202111001309 A CN 202111001309A CN 114307866 A CN114307866 A CN 114307866A
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Abstract
The invention relates to a novel reaction system of a propane dehydrogenation device, which adopts a high-efficiency heat exchanger for feeding and discharging reaction, directly preheats a raw material gas from a high-temperature reaction gas at the outlet of a reactor, improves the feeding temperature of the raw material gas, reduces the consumption of fuel gas in a heating furnace, effectively improves the utilization efficiency of high-grade energy in the reaction system, and also reduces the emission of flue gas and tail gas of the device; meanwhile, the axial and radial fixed bed reactor has the characteristics of small reaction pressure drop, small occupied area, low catalyst loss, low investment cost, high reaction conversion rate and the like. In the arrangement process, the inlet and outlet heat exchangers are arranged in parallel and close to the propane dehydrogenation reactor, so that the length of a high-temperature pipeline of the product gas is reduced, and the thermal cracking and coking processes of the product gas in the high-temperature pipeline are reduced.
Description
Technical Field
The invention relates to a novel reaction system of a propane dehydrogenation device.
Background
In the mainstream propane dehydrogenation process at present, high-temperature gas at the outlet of a reactor is firstly divided into two parts in a reaction system, one part is used for producing high-pressure steam as a byproduct, and then the two parts are mixed and preheated to obtain reaction feed gas. However, in the heat exchange process, the temperature of the high-temperature gas at the outlet of the reactor is high, the temperature difference of the high-pressure steam by-product is large, the utilization efficiency of high-grade energy is low, the two high-temperature and low-temperature reaction outlet gases are mixed, the quality of energy is greatly reduced, and the defects of serious high-grade energy loss and the like exist.
In the current mainstream process, a reactor in a reaction system mainly adopts a fluidized bed type or horizontal fixed bed type propane dehydrogenation reactor. The fluidized bed type propane dehydrogenation reactor is similar to a series connection type of a plurality of vertical radial reactors, and has the defects of high equipment investment, serious catalyst abrasion, low propylene yield and the like. The horizontal fixed bed propane dehydrogenation reactor adopts a reaction operation process in which a plurality of horizontal fixed bed reactors are connected in parallel, and has the problems of large floor area, complex piping, large bed pressure drop, high energy consumption of movable equipment and the like.
For example, patent No. CN201180013906.1, new reactor scheme for dehydrogenating propane to propylene, proposes a method for dehydrogenating paraffin, which uses two fluidized bed type reactors with on-line switching of reaction regeneration, and has the disadvantages of high equipment requirement and serious catalyst loss. A propane dehydrogenation device and a propane dehydrogenation method are proposed in patent application No. CN201810148953.0, namely propane dehydrogenation device and method; the patent CN201720974768.8 'efficient heat exchanger for feeding and discharging materials of propane dehydrogenation device reactor' provides an efficient heat exchanger for feeding and discharging materials of propane dehydrogenation device reactor with good heat exchange effect and low use cost. However, the process flow in the two schemes is the same as that of the existing mainstream propane dehydrogenation device, namely high-temperature reaction gas at the outlet of the reactor is partially shunted to generate high-pressure steam as a byproduct, and the defects of low high-grade energy utilization efficiency generally exist.
In addition, in the arrangement of the existing device, the arrangement position of the inlet and outlet heat exchangers is far away from the position of the propane dehydrogenation reactor, and a long high-temperature pipeline of the product gas exists, so that the problems of thermal cracking and serious coking of the high-temperature product gas in the pipeline can be caused.
Disclosure of Invention
The invention aims to solve the technical problem of the prior art and provides a novel reaction system of a propane dehydrogenation device, which has the advantages of high energy utilization efficiency, high reaction conversion rate, small occupied area of the device, low catalyst loss, low investment cost and low pollutant emission.
The technical scheme adopted by the invention for solving the technical problems is as follows: a novel reaction system of a propane dehydrogenation device is characterized in that:
preheating a fresh propane raw material by at least three parallel feed and discharge heat exchangers E-101A, E-101B and E-101C, and reheating the preheated raw material gas by a heating furnace H-101;
sending the obtained high-temperature raw material gas to an axial-radial propane dehydrogenation reactor R-101A and an axial-radial propane dehydrogenation reactor R-101B;
high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A is mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, and then enters a charging and discharging heat exchanger E-101A, a charging and discharging heat exchanger E-101B and a charging and discharging heat exchanger E-101C to directly preheat feed gas, and the obtained product gas is sent to a separation and recovery system.
Preferably, the reaction charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are efficient heat exchangers, and the heat exchangers are efficient wound tube type heat exchangers or efficient plate type heat exchangers; the arrangement positions of the reaction charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are parallel and close to the propane dehydrogenation reactor R-101A, so that the length of a high-temperature pipeline at a product gas outlet is reduced, and thermal cracking and coking of the product gas at high temperature are reduced.
Preferably, the operation conditions of hot side inlets of the feeding and discharging heat exchanger E-101A, the feeding and discharging heat exchanger E-101B and the feeding and discharging heat exchanger E-101C are 450-550 ℃, 50-300 kPag and 100-150 ℃, and 50-300 kPag; the cold side inlet operation conditions of the charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are 30-50 ℃ and 300-600 kPag, and the cold side outlet operation conditions are 400-500 ℃ and 200-400 kPag.
Preferably, in the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B, reaction catalysts are arranged in a fixed bed annular axial mode.
Preferably, the flow modes of the materials in the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B are up-in-down-out, down-in-up-out, middle-in-up-down-out or up-in-up-down-in-middle-out.
Preferably, the reaction conditions of the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B are that the reaction temperature is 500-650 ℃, and the reaction pressure is-50 kPag-300 kPag.
Preferably, the reaction system of the invention further comprises a feed and discharge heat exchanger E-101D, and the feed and discharge heat exchanger E-101D is connected in parallel with the feed and discharge heat exchanger E-101A, the feed and discharge heat exchanger E-101B and the feed and discharge heat exchanger E-101C.
In the invention, high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A is mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, and then sequentially enters a charging and discharging heat exchanger E-101A, a charging and discharging heat exchanger E-101B, a charging and discharging heat exchanger E-101C and a charging and discharging heat exchanger E-101D from the bottom to directly preheat feed gas.
Preferably, high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A firstly enters a feeding and discharging heat exchanger E-101A and a feeding and discharging heat exchanger E-101B for primary heat recovery, after being mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, two outlet materials at the tops of the feeding and discharging heat exchanger E-101A and the feeding and discharging heat exchanger E-101B are respectively mixed with two paths of reduction purge steam which come from the bottom of the axial-radial propane dehydrogenation reactor R-101B and are subjected to flow division, and are sent to a feeding and discharging heat exchanger E-101C and a feeding and discharging heat exchanger E-101D for secondary heat recovery, and two paths of product gas obtained by the feeding and discharging heat exchanger E-101C and the feeding and discharging heat exchanger E-101D are subjected to mixed separation system.
The reaction charging and discharging heat exchanger directly and sequentially preheats the reaction charging propane material flow by taking high-temperature reaction gas at the outlet of the reactor as a heat source.
Compared with the prior art, the invention has the advantages that: the high-efficiency heat exchanger for feeding and discharging in the reaction is adopted, and the high-temperature reaction gas at the outlet of the reactor directly preheats the raw material gas, so that the feeding temperature of the raw material gas is improved, the consumption of the fuel gas in the heating furnace is reduced, the utilization efficiency of high-grade energy in the reaction system is effectively improved, and the emission of the tail gas of the flue gas of the device is reduced; meanwhile, the axial and radial fixed bed reactor has the characteristics of small reaction pressure drop, small occupied area, low catalyst loss, low investment cost, high reaction conversion rate and the like. In the arrangement process, the inlet and outlet heat exchangers are arranged in parallel and close to the propane dehydrogenation reactor, so that the length of a high-temperature pipeline of the product gas is reduced, and the thermal cracking and coking processes of the product gas in the high-temperature pipeline are reduced.
Drawings
FIG. 1 is a flowchart of example 1 of the present invention;
FIG. 2 is a flowchart of example 2 of the present invention;
fig. 3 is a flowchart of embodiment 3 of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
Example 1:
as shown in fig. 1, the novel reaction system of the propane dehydrogenation apparatus of this embodiment is:
preheating a fresh propane raw material by three parallel feed and discharge heat exchangers E-101A, E-101B and E-101C, and reheating the preheated raw material gas by a heating furnace H-101;
sending the obtained high-temperature raw material gas to an axial-radial propane dehydrogenation reactor R-101A and an axial-radial propane dehydrogenation reactor R-101B;
high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A is mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, and then enters a charging and discharging heat exchanger E-101A, a charging and discharging heat exchanger E-101B and a charging and discharging heat exchanger E-101C to directly preheat feed gas, and the obtained product gas is sent to a separation and recovery system.
The reaction charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are high-efficiency heat exchangers, and the heat exchangers are high-efficiency wound tube type heat exchangers or high-efficiency plate type heat exchangers; the arrangement positions of the reaction charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are parallel and close to the propane dehydrogenation reactor R-101A, so that the length of a high-temperature pipeline at a product gas outlet is reduced, and thermal cracking and coking of the product gas at high temperature are reduced.
The hot side inlet operation conditions of the charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are 450-550 ℃, 50-300 kPag and 100-150 ℃, and 50-300 kPag; the cold side inlet operation conditions of the charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are 30-50 ℃ and 300-600 kPag, and the cold side outlet operation conditions are 400-500 ℃ and 200-400 kPag.
In the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B, reaction catalysts are arranged in a fixed bed annular axial mode.
The flow modes of the materials in the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B are up-in-down-out, down-in-up-out, middle-in-up-down-out or up-down-in-middle-out.
The reaction conditions of the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B are that the reaction temperature is 500-650 ℃, and the reaction pressure is-50 kPag-300 kPag.
The embodiment is a novel reaction system of a propane dehydrogenation device, which adopts an axial and radial fixed bed reactor and is combined with a reaction feed-discharge heat exchanger to directly preheat feed gas. Taking a 60 ten thousand ton/year-scale propane dehydrogenation device as an example, a fluidized bed and a moving bed reactor are adopted, the catalyst loss amounts are respectively 600-650 ton/year and 10-15 ton/year, and the catalyst loss of a horizontal fixed bed reactor and an axial and radial fixed bed reactor is almost zero. However, the horizontal fixed bed reactor occupies a large area, the classical arrangement of the horizontal fixed bed reactor occupies an area of 1500-2700 m2, the arrangement of the fluidized bed reactor occupies an area of 800-1200 m2, and the axial and radial fixed bed reactor provided by the embodiment occupies an area of only 400-600 m 2. Meanwhile, the bed pressure drop of the fluidized bed, the moving bed and the horizontal fixed bed reactor is between 50kPa and 80kPa, and the bed pressure drop of the axial and radial fixed bed reactor provided by the embodiment is only 10 kPa to 20 kPa. Meanwhile, the high-temperature reaction gas is used as a heat source to directly preheat the raw material by adopting the high-efficiency heat exchanger, so that the energy consumption of the heating furnace can be effectively reduced by 17.57 MW-21.47 MW, and the operation cost can be reduced by 1577.1-1927.6 ten thousand yuan/year.
The data table 1 of the inlet and outlet material flows of the novel reaction system of the propane dehydrogenation device in the embodiment is as follows:
TABLE 1 data sheet of inlet and outlet material flows of novel reaction system of propane dehydrogenation device with three parallel inlet and outlet material heat exchangers and axial and radial reactors
The conversion rate of propane can reach 46% by calculation, and the selectivity is more than 87%.
Through calculation, the structural dimensions of a single downward-entering and upward-exiting axial-radial propane dehydrogenation reactor of a 60-ten-thousand-ton propane dehydrogenation device are shown in table 2:
TABLE 2 reactor configuration size data sheet
Example 2:
as shown in fig. 2, compared with embodiment 1, the reaction system of this embodiment further includes a feed/discharge heat exchanger E-101D, where the feed/discharge heat exchanger E-101D is connected in parallel with the feed/discharge heat exchanger E-101A, the feed/discharge heat exchanger E-101B, and the feed/discharge heat exchanger E-101C.
High-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A is mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, and then sequentially enters a charging and discharging heat exchanger E-101A, a charging and discharging heat exchanger E-101B, a charging and discharging heat exchanger E-101C and a charging and discharging heat exchanger E-101D from the bottom to directly preheat raw material gas.
Example 3:
this example differs from example 2 in that: as shown in figure 3, high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A firstly enters a feeding and discharging heat exchanger E-101A and a feeding and discharging heat exchanger E-101B for primary heat recovery, after being mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, two outlet materials at the tops of the feeding and discharging heat exchanger E-101A and the feeding and discharging heat exchanger E-101B are respectively mixed with two paths of reduction purge steam which come from the bottom of the axial-radial propane dehydrogenation reactor R-101B and are subjected to shunting, the mixture is sent to a feeding and discharging heat exchanger E-101C and a feeding and discharging heat exchanger E-101D for secondary heat recovery, and product gas obtained by the feeding and discharging heat exchanger E-101C and the feeding and discharging heat exchanger E-101D is subjected to a separation system after being mixed.
The reaction charging and discharging heat exchanger directly and sequentially preheats the reaction charging propane material flow by taking high-temperature reaction gas at the outlet of the reactor as a heat source.
Claims (10)
1. A novel reaction system of a propane dehydrogenation device is characterized in that:
preheating a fresh propane raw material by at least three parallel feed and discharge heat exchangers E-101A, E-101B and E-101C, and reheating the preheated raw material gas by a heating furnace H-101;
sending the obtained high-temperature raw material gas to an axial-radial propane dehydrogenation reactor R-101A and an axial-radial propane dehydrogenation reactor R-101B;
high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A is mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, and then enters a charging and discharging heat exchanger E-101A, a charging and discharging heat exchanger E-101B and a charging and discharging heat exchanger E-101C to directly preheat feed gas, and the obtained product gas is sent to a separation and recovery system.
2. The novel reaction system of a propane dehydrogenation unit according to claim 1, characterized in that: the reaction charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are high-efficiency heat exchangers, and the heat exchangers are high-efficiency wound tube type heat exchangers or high-efficiency plate type heat exchangers; the arrangement positions of the reaction charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are parallel and close to the propane dehydrogenation reactor R-101A, so that the length of a high-temperature pipeline at a product gas outlet is reduced, and thermal cracking and coking of the product gas at high temperature are reduced.
3. The novel reaction system of a propane dehydrogenation unit according to claim 2, characterized in that: the hot side inlet operation conditions of the charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are 450-550 ℃, 50-300 kPag and 100-150 ℃, and 50-300 kPag; the cold side inlet operation conditions of the charging and discharging heat exchanger E-101A, the charging and discharging heat exchanger E-101B and the charging and discharging heat exchanger E-101C are 30-50 ℃ and 300-600 kPag, and the cold side outlet operation conditions are 400-500 ℃ and 200-400 kPag.
4. The novel reaction system of a propane dehydrogenation unit according to claim 1, characterized in that: in the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B, reaction catalysts are arranged in a fixed bed annular axial mode.
5. The novel reaction system of a propane dehydrogenation unit according to claim 4, characterized in that: the flow modes of the materials in the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B are up-in-down-out, down-in-up-out, middle-in-up-down-out or up-down-in-middle-out.
6. The novel reaction system of a propane dehydrogenation unit according to claim 4, characterized in that: the reaction conditions of the axial-radial propane dehydrogenation reactor R-101A and the axial-radial propane dehydrogenation reactor R-101B are that the reaction temperature is 500-650 ℃, and the reaction pressure is-50 kPag-300 kPag.
7. The novel reaction system of a propane dehydrogenation unit according to claim 1, characterized in that: the heat exchanger E-101D is connected with the heat exchanger E-101A, the heat exchanger E-101B and the heat exchanger E-101C in parallel.
8. The novel reaction system of a propane dehydrogenation unit according to claim 7, characterized in that: high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A is mixed with reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, and then sequentially enters a charging and discharging heat exchanger E-101A, a charging and discharging heat exchanger E-101B, a charging and discharging heat exchanger E-101C and a charging and discharging heat exchanger E-101D from the bottom to directly preheat feed gas.
9. The novel reaction system of a propane dehydrogenation unit according to claim 7, characterized in that: the high-temperature reaction gas at the outlet of the axial-radial propane dehydrogenation reactor R-101A firstly enters a feeding and discharging heat exchanger E-101A and a feeding and discharging heat exchanger E-101B for primary heat recovery, is mixed with the reduction purge steam of the axial-radial propane dehydrogenation reactor R-101B, then two outlet materials at the tops of the feeding and discharging heat exchanger E-101A and the feeding and discharging heat exchanger E-101B are respectively mixed with the two split reduction purge steam from the bottom of the axial-radial propane dehydrogenation reactor R-101B, and are sent to a feeding and discharging heat exchanger E-101C and a feeding and discharging heat exchanger E-101D for secondary heat recovery, and two product gases obtained by the feeding and discharging heat exchanger E-101C and the feeding and discharging heat exchanger E-101D are mixed to obtain a separation system.
10. The novel reaction system of a propane dehydrogenation unit according to claim 9, characterized in that: the reaction charging and discharging heat exchanger directly and sequentially preheats the reaction charging propane material by taking high-temperature reaction gas at the outlet of the reactor as a heat source.
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