Disposal system for liquid discharged from compressor in high-pressure hydrogenation process of 1, 4-butanediol device

Abstract

The invention discloses a treatment system for liquid discharged from a compressor in a high-pressure hydrogenation process of a 1, 4-butanediol device, and belongs to the technical field of chemical engineering. The disposal system comprises a hydrogen compressor inlet separator and multiple stages of hydrogen compressor compression sections, the hydrogen compressor inlet separator 1 is connected with a raw material hydrogen conveying line, and each hydrogen compressor compression section comprises a hydrogen compressor compression cylinder, a cooler and a separator which are sequentially connected in the hydrogen flowing direction. Wherein the hydrogen compressor compression cylinder of the first section is connected with the hydrogen compressor inlet separator, and the separator of the last section is connected with the high-pressure hydrogenation reactor through a pipeline; the treatment system further comprises a condensate discharging flash tank, the liquid discharging pipeline of each section of separator is connected to the condensate discharging flash tank, and each liquid discharging pipeline is provided with a Venturi nozzle. According to the treatment system, the safety and stability of the high-pressure hydrogenation process can be improved, the operation risk is reduced, and the hydrogen consumption and the sewage treatment risk are reduced.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical industry, and in particular relates to a disposal system for liquid discharge from a compressor in a high-pressure hydrogenation process of a 1,4-butanediol device. Background Art

[0002] 1,4-Butanediol (BDO) is an important basic organic chemical and fine chemical raw material with a wide range of applications. Existing technology primarily produces 1,4-butanediol using the acetylene-aldehyde process. In this process, acetylene reacts with formaldehyde to produce 1,4-butynediol (BYD). After filtration and distillation to remove impurities such as methanol and formaldehyde, BYD is hydrogenated with hydrogen in a BDO reactor to produce 1,4-butanediol (BDO).

[0003] In the 1,4-butanediol production process using the acetylene aldehyde method, the high-pressure hydrogenation process is a key step. Here, 1,4-butynediol (BYD) and hydrogen undergo a hydrogenation reaction in a reactor to produce 1,4-butanediol (BDO). The hydrogenation reaction temperature ranges from 90 to 145°C, and the pressure reaches up to 305 kg / cm 2 G. In order to meet the reaction requirements, the raw hydrogen is compressed to 308kg / cm3 by a reciprocating hydrogen compressor. 2 G, and then the circulating gas compressor outlet pressure is 306.5kg / cm 2 The recycled gas of G is mixed and finally sent to the BDO high-pressure hydrogenation reactor.

[0004] During the compression process, separators between each stage of the reciprocating hydrogen compressor and at the inlet of the recycle gas compressor are used to separate and discharge condensate from the compressed gas to prevent damage to the compressor caused by liquid carryover from the gas. Existing systems typically use a level-controlled regulating valve to discharge condensate, with the discharged condensate collected in an atmospheric condensate tank and sent to a wastewater treatment facility.

[0005] However, during the high-pressure hydrogenation process, due to the extremely high operating pressures of the compressor's separators at each stage and the large fluctuations in condensate production, the associated liquid-level control valves are subjected to long-term operating conditions characterized by high pressure differentials and frequent opening changes. This leads to severe valve core scouring and frequent failures, seriously impacting the compressor's continuous and stable operation. Furthermore, when the control valve fails, the separator liquid level may become empty, causing large amounts of high-pressure hydrogen to escape into the downstream atmospheric pressure system, potentially causing equipment overpressure, fire, and other safety incidents. Furthermore, the hydrogen dissolved in the condensate is directly discharged into the sewage treatment system, increasing both hydrogen consumption and the risks associated with the treatment of hydrogen-containing wastewater.

[0006] Therefore, providing a disposal system for the compressor discharge liquid in the high-pressure hydrogenation process of the 1,4-butanediol unit to improve the safety and stability of the high-pressure hydrogenation process, reduce operational risks, and reduce hydrogen consumption and wastewater treatment risks has become an urgent problem to be solved by those skilled in the art. Summary of the Invention

[0007] The purpose of the present invention is to provide a system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol unit, so as to solve the problems of difficult operation and control, high safety risk and poor stability in the prior art.

[0008] To achieve the above object, the technical solution adopted by the present invention is as follows:

[0009] The present invention discloses a system for disposing liquid discharge from a compressor in a high-pressure hydrogenation process of a 1,4-butanediol device, comprising a hydrogen compressor inlet separator and a multi-stage hydrogen compressor compression section. The hydrogen compressor inlet separator is connected to a raw hydrogen gas transmission line. Each hydrogen compressor compression section comprises a hydrogen compressor compression cylinder, a cooler, and a separator connected in sequence according to the flow direction of hydrogen. The hydrogen compressor compression cylinder of the first section is connected to the hydrogen compressor inlet separator, and the separator of the last section is connected to a high-pressure hydrogenation reactor via a pipeline.

[0010] The treatment system further includes a condensate flash tank, the discharge pipelines of each separator section are connected to the condensate flash tank, and each discharge pipeline is provided with a Venturi nozzle.

[0011] In some embodiments of the present invention, a full-bore switch valve is provided on the discharge pipeline of each section, downstream of the venturi nozzle, and its diameter matches the outlet of the venturi nozzle. The full-bore switch valve is controlled to open and close by the separator liquid level interlock system within this section.

[0012] In some embodiments of the present invention, the separator liquid level interlock system of each section includes a liquid level monitor provided on the separator, and a controller connected to the liquid level monitor and the full-bore switch valve respectively; preferably, the interlock threshold is set to 20% to 80% of the liquid level.

[0013] In some embodiments of the present invention, a replaceable anti-scour orifice plate is provided on the drainage pipeline of each work section, downstream of the full-bore switch valve, and the outlet pipeline of the anti-scour orifice plate is connected to the flash tank; preferably, the replaceable anti-scour orifice plate adopts an eccentric porous array structure; more preferably, the pore size gradient distribution of the replaceable anti-scour orifice plate is ≤20%.

[0014] In some embodiments of the present invention, a circulating gas treatment section is further included, which includes a circulating gas separator and a circulating gas compressor; the gas outlet of the high-pressure hydrogenation reactor is connected to the circulating gas separator via a pipeline, the gas outlet of the circulating gas separator is connected to the circulating gas compressor via a pipeline, and the gas outlet of the circulating gas compressor is connected to the high-pressure hydrogenation reactor via a pipeline; the discharge pipeline of the circulating gas separator is connected to the condensate flash tank, and a Venturi nozzle is provided on the discharge pipeline of the circulating gas separator.

[0015] In some embodiments of the present invention, a full-bore on-off valve is provided on the discharge line of the circulating gas separator, downstream of the venturi nozzle, and its diameter matches the outlet of the venturi nozzle. The full-bore on-off valve is controlled by the separator liquid level interlock system in this section.

[0016] Preferably, the liquid level interlock system of the circulating gas separator includes a liquid level monitor provided on the circulating gas separator, and a controller connected to the liquid level monitor and the full-bore switch valve respectively; preferably, the interlock threshold is set to 20% to 80% of the liquid level;

[0017] Preferably, a replaceable anti-scour orifice plate is provided on the discharge line of the circulating gas separator, downstream of the full-bore switch valve, and the outlet pipeline of the anti-scour orifice plate is connected to the flash tank; more preferably, the replaceable anti-scour orifice plate adopts an eccentric porous array structure; further preferably, the pore size gradient distribution of the replaceable anti-scour orifice plate has an opening rate of ≤20%.

[0018] In some embodiments of the present invention, the gas phase pipeline on the top of the condensate flash tank is connected to the separator at the inlet of the hydrogen compressor;

[0019] A liquid level joint control valve is installed at the bottom of the condensate flash tank to discharge the condensate after analysis into the atmospheric pressure condensate tank, and finally into the sewage treatment system through pumping.

[0020] In some embodiments of the present invention, the discharge line of the separator at the inlet of the hydrogen compressor is connected to the atmospheric condensate tank.

[0021] In some embodiments of the present invention, the multi-stage hydrogen compressor has four compression sections.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] The present invention has a scientific design and an ingenious conception. By adopting the compressor discharge disposal system of the high-pressure hydrogenation process of the 4-butanediol device of the present invention, the safety and stability of the high-pressure hydrogenation process can be improved, the operation risk can be reduced, and the hydrogen consumption and sewage treatment risks can be reduced.

[0024] The present invention adopts the coordinated design of full-bore switch valve and replaceable anti-scour orifice plate to eliminate the erosion problem of regulating valve and extend the comprehensive maintenance cycle to more than 3 times of the original system;

[0025] The present invention adopts a dual barrier of a Venturi nozzle + a full-bore switch valve to prevent accidental leakage of high-pressure hydrogen and reduce the risk of safety accidents by 95%.

[0026] The system of the present invention can achieve efficient resource utilization: the hydrogen recovery rate is increased to 92% to 95%, and the annual hydrogen consumption cost is saved by about 1.5 million yuan (based on an annual production capacity of 100,000 tons).

[0027] By adopting the system of the present invention, the dissolved hydrogen concentration in the sewage system is ≤5ppm, which meets the limit requirements of GB 31571-2015 "Petrochemical Industry Pollutant Emission Standard". BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Attachment Figure 1 Schematic diagram of the system structure of the present invention.

[0029] The names corresponding to the reference numerals are:

[0030] 1-hydrogen compressor inlet separator, 2-condensate flash tank, 3-high-pressure hydrogenation reactor, 4-normal-pressure condensate tank, 5-pump;

[0031] 11 / 21 / 31 / 41-Hydrogen compressor cylinder, 12 / 22 / 32 / 42-Separator, 13 / 23 / 33 / 43-Venturi nozzle, 14 / 24 / 34 / 44-Full-bore on-off valve, 15 / 25 / 35 / 45-Anti-scour orifice plate, 16 / 26 / 36 / 46-Liquid level monitor, 17 / 27 / 37 / 47-Controller, 18 / 28 / 38 / 48-Cooler;

[0032] 51 - circulating gas compressor; 52 - circulating gas separator, 53 - Venturi nozzle, 54 - full-bore on-off valve, 55 - replaceable anti-scour orifice plate, 56 - circulating gas separator liquid level monitor, 57 - circulating gas treatment section controller;

[0033] 100-condensate drain main, 101 / 102 / 103 / 104-drain lines, 105-circulating gas separator drain line. DETAILED DESCRIPTION

[0034] In order to make the objectives, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings. Obviously, the embodiments described are only some embodiments of the present invention, not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.

[0035] Example 1

[0036] As attached Figure 1 As shown, this embodiment discloses a system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol device, comprising a hydrogen compressor inlet separator 1 and a multi-stage hydrogen compressor compression section, wherein the multi-stage hydrogen compressor compression section is four-stage. The hydrogen compressor inlet separator 1 is connected to a raw hydrogen delivery line. Each section of the hydrogen compressor compression section comprises a hydrogen compressor compression cylinder 11 / 21 / 31 / 41, a cooler 18 / 28 / 38 / 48 and a separator 12 / 22 / 32 / 42 connected in sequence according to the flow direction of hydrogen, wherein the hydrogen compressor compression cylinder 11 of the first section is connected to the hydrogen compressor inlet separator 1, and the separator 42 of the last section is connected to the high-pressure hydrogenation reactor 3 via a pipeline;

[0037] The treatment system further includes a condensate flash tank 2, and the discharge pipelines 101 / 102 / 103 / 104 of each separator section are connected to the condensate flash tank 2, and each discharge pipeline is provided with a venturi nozzle 13 / 23 / 33 / 43.

[0038] The present invention's compressor discharge disposal system for the high-pressure hydrogenation process of a 1,4-butanediol plant improves the safety and stability of the process, reduces operational risks, and minimizes hydrogen consumption and wastewater disposal risks. The system utilizes a Venturi nozzle for discharge. Designed based on the dynamic characteristics of gas-liquid two-phase flow, the nozzle throat diameter and flow channel inclination angle meet critical flow conditions, enabling quantitative discharge of separator condensate and forming a dynamic gas-liquid two-phase seal to prevent hydrogen leakage.

[0039] Example 2

[0040] As attached Figure 1 As shown, this embodiment discloses a system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol device, comprising a hydrogen compressor inlet separator 1 and a multi-stage hydrogen compressor compression section, wherein the multi-stage hydrogen compressor compression section is four-stage. The hydrogen compressor inlet separator 1 is connected to a raw hydrogen delivery line, and each section of the hydrogen compressor compression section comprises a hydrogen compressor compression cylinder 11 / 21 / 31 / 41, a cooler 18 / 28 / 38 / 48 and a separator 12 / 22 / 32 / 42 connected in sequence according to the flow direction of hydrogen, wherein the hydrogen compressor compression cylinder 11 of the first section is connected to the hydrogen compressor inlet separator 1, and the separator 42 of the last section is connected to the high-pressure hydrogenation reactor 3 via a pipeline;

[0041] The treatment system further includes a condensate flash tank 2, and the discharge pipelines 101 / 102 / 103 / 104 of each separator section are connected to the condensate flash tank 2, and each discharge pipeline is provided with a venturi nozzle 13 / 23 / 33 / 43.

[0042] A full-bore switch valve 14 / 24 / 34 / 44 is installed on the discharge pipeline 101 / 102 / 103 / 104 of each section, downstream of the Venturi nozzle 13 / 23 / 33 / 43. Its diameter matches the Venturi nozzle outlet on the same discharge pipeline. The full-bore switch valve 14 / 24 / 34 / 44 is controlled to open and close by the separator liquid level interlock system within this section.

[0043] The separator liquid level interlocking system of each section includes a liquid level monitor 16 / 26 / 36 / 46 arranged on the separator 12 / 22 / 32 / 42, and a controller 17 / 27 / 37 / 47 connected to the liquid level monitor 16 / 26 / 36 / 46 and the full-bore switch valve 14 / 24 / 34 / 44 respectively; preferably, the interlocking threshold is set to 20% to 80% of the liquid level.

[0044] Based on Example 1, this Example 2 provides a more preferred technical solution. Specifically: A full-bore switch valve is provided on the discharge pipeline of each section, downstream of the venturi nozzle, and its diameter matches the outlet of the venturi nozzle. The full-bore switch valve is controlled to open and close by the separator liquid level interlock system in this section. The separator liquid level interlock system of each section includes a liquid level monitor provided on the separator, and a controller connected to the liquid level monitor and the full-bore switch valve respectively; the interlock threshold is set to 20% to 80% of the liquid level. This embodiment installs a full-bore switch valve downstream of the venturi nozzle, and its diameter matches the nozzle outlet. The separator liquid level interlock control opens and closes the interlock threshold to 20% to 80% of the liquid level, ensuring zero leakage in the high-pressure stage and avoiding wear caused by frequent operation.

[0045] Example 3

[0046] As attached Figure 1 As shown, this embodiment discloses a system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol device, comprising a hydrogen compressor inlet separator 1 and a multi-stage hydrogen compressor compression section, wherein the multi-stage hydrogen compressor compression section is four-stage. The hydrogen compressor inlet separator 1 is connected to a raw hydrogen delivery line, and each section of the hydrogen compressor compression section comprises a hydrogen compressor compression cylinder 11 / 21 / 31 / 41, a cooler 18 / 28 / 38 / 48 and a separator 12 / 22 / 32 / 42 connected in sequence according to the flow direction of hydrogen, wherein the hydrogen compressor compression cylinder 11 of the first section is connected to the hydrogen compressor inlet separator 1, and the separator 42 of the last section is connected to the high-pressure hydrogenation reactor 3 via a pipeline;

[0047] The treatment system further includes a condensate flash tank 2, and the discharge pipelines 101 / 102 / 103 / 104 of each separator section are connected to the condensate flash tank 2, and each discharge pipeline is provided with a venturi nozzle 13 / 23 / 33 / 43.

[0048] A full-bore switch valve 14 / 24 / 34 / 44 is installed on the discharge pipeline 101 / 102 / 103 / 104 of each section, downstream of the Venturi nozzle 13 / 23 / 33 / 43. Its diameter matches the Venturi nozzle outlet on the same discharge pipeline. The full-bore switch valve 14 / 24 / 34 / 44 is controlled to open and close by the separator liquid level interlock system within this section.

[0049] The separator liquid level interlocking system of each section includes a liquid level monitor 16 / 26 / 36 / 46 arranged on the separator 12 / 22 / 32 / 42, and a controller 17 / 27 / 37 / 47 connected to the liquid level monitor 16 / 26 / 36 / 46 and the full-bore switch valve 14 / 24 / 34 / 44 respectively; preferably, the interlocking threshold is set to 20% to 80% of the liquid level.

[0050] A replaceable anti-scour orifice plate 15 / 25 / 35 / 45 is installed on the drainage pipeline 101 / 102 / 103 / 104 of each work section, downstream of the full-bore switch valve 14 / 24 / 34 / 44, and the outlet pipeline of the anti-scour orifice plate 15 / 25 / 35 / 45 is connected to the condensate flash tank 2; the replaceable anti-scour orifice plate 15 / 25 / 35 / 45 adopts an eccentric porous array structure; the pore size is gradiently distributed, and the open porosity is ≤20%.

[0051] This embodiment 3 provides a more preferred technical solution based on embodiment 2. Specifically, a replaceable anti-scour orifice plate is installed on the drainage pipeline of each work section, downstream of the full-bore switch valve, and the outlet pipeline of the anti-scour orifice plate is connected to the flash tank. The replaceable anti-scour orifice plate adopts an eccentric multi-porous array structure with a pore size gradient distribution and an open porosity of ≤20%. This embodiment 3 connects the replaceable anti-scour orifice plate in series downstream of the full-bore switch valve. The orifice plate adopts an eccentric multi-porous array structure with a pore size gradient distribution and an open porosity of ≤20%. Through multi-stage eddy diffusion, the high-pressure condensate kinetic energy is absorbed and the pressure is reduced by throttling, thereby reducing erosion of the downstream pipeline.

[0052] Example 4

[0053] As attached Figure 1 As shown, this embodiment discloses a system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol device, comprising a hydrogen compressor inlet separator 1 and a multi-stage hydrogen compressor compression section, wherein the multi-stage hydrogen compressor compression section is four-stage. The hydrogen compressor inlet separator 1 is connected to a raw hydrogen delivery line, and each section of the hydrogen compressor compression section comprises a hydrogen compressor compression cylinder 11 / 21 / 31 / 41, a cooler 18 / 28 / 38 / 48 and a separator 12 / 22 / 32 / 42 connected in sequence according to the flow direction of hydrogen, wherein the hydrogen compressor compression cylinder 11 of the first section is connected to the hydrogen compressor inlet separator 1, and the separator 42 of the last section is connected to the high-pressure hydrogenation reactor 3 via a pipeline;

[0054] The treatment system further includes a condensate flash tank 2, and the discharge pipelines 101 / 102 / 103 / 104 of each separator section are connected to the condensate flash tank 2, and each discharge pipeline is provided with a venturi nozzle 13 / 23 / 33 / 43.

[0055] A full-bore switch valve 14 / 24 / 34 / 44 is installed on the discharge pipeline 101 / 102 / 103 / 104 of each section, downstream of the Venturi nozzle 13 / 23 / 33 / 43. Its diameter matches the Venturi nozzle outlet on the same discharge pipeline. The full-bore switch valve 14 / 24 / 34 / 44 is controlled to open and close by the separator liquid level interlock system within this section.

[0056] The separator liquid level interlocking system of each section includes a liquid level monitor 16 / 26 / 36 / 46 installed on the separator 12 / 22 / 32 / 42, and a controller 17 / 27 / 37 / 47 connected to the liquid level monitor 16 / 26 / 36 / 46 and the full-bore switch valve 14 / 24 / 34 / 44 respectively; the interlocking threshold is set at 20% to 80% of the liquid level.

[0057] A replaceable anti-scour orifice plate 15 / 25 / 35 / 45 is installed on the drainage pipeline 101 / 102 / 103 / 104 of each work section, downstream of the full-bore switch valve 14 / 24 / 34 / 44, and the outlet pipeline of the anti-scour orifice plate 15 / 25 / 35 / 45 is connected to the condensate flash tank 2; the replaceable anti-scour orifice plate 15 / 25 / 35 / 45 adopts an eccentric porous array structure; the pore size is gradiently distributed, and the open porosity is ≤20%.

[0058] The disposal system of this embodiment also includes a circulating gas treatment section, which includes a circulating gas separator 52 and a circulating gas compressor 51; the gas outlet of the high-pressure hydrogenation reactor 3 is connected to the circulating gas separator 52 via a pipeline, the gas outlet of the circulating gas separator 52 is connected to the circulating gas compressor 51 via a pipeline, and the gas outlet of the circulating gas compressor 51 is connected to the high-pressure hydrogenation reactor 3 via a pipeline; the circulating gas separator discharge pipeline 105 is connected to the condensate flash tank 2.

[0059] The circulating gas separator discharge line 105 is equipped with a Venturi nozzle 53, a full-bore on-off valve 54, and a replaceable anti-scour orifice plate 55, arranged in sequence according to the material flow direction. The full-bore on-off valve 54 has a diameter that matches the outlet of the Venturi nozzle 53, and its opening and closing are controlled by the circulating gas separator liquid level interlock system. The circulating gas separator liquid level interlock system includes a circulating gas separator liquid level monitor 56 installed on the circulating gas separator 52, and a circulating gas treatment section controller 57 connected to the circulating gas separator liquid level monitor 56 and the full-bore on-off valve 54, respectively. The interlock threshold is set at 20% to 80% of the liquid level. The outlet pipeline of the anti-scour orifice plate 55 is connected to the flash tank 2 through the condensate main pipe 100. The anti-scour orifice plate 55 adopts an eccentric multi-porous array structure with a gradient pore size distribution and an open porosity of ≤20%.

[0060] This embodiment 4 provides a more preferred technical solution based on embodiment 3. Specifically, the disposal system of this embodiment also includes a circulating gas treatment section, and defines the specific composition of the circulating gas treatment section. This embodiment uses a Venturi nozzle for drainage in the circulating gas treatment section, installs a full-bore switch valve downstream of the Venturi nozzle, and connects a replaceable anti-scour orifice plate in series downstream of the full-bore switch valve. This design can achieve quantitative discharge of condensate from the separator in the circulating gas treatment section, form a gas-liquid two-phase dynamic seal, block hydrogen leakage, ensure zero leakage in the high-pressure stage and avoid wear caused by frequent operation, and reduce erosion of downstream pipelines.

[0061] Example 5

[0062] As attached Figure 1 As shown, this embodiment discloses a system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol device, comprising a hydrogen compressor inlet separator 1 and a multi-stage hydrogen compressor compression section, wherein the multi-stage hydrogen compressor compression section is four-stage. The hydrogen compressor inlet separator 1 is connected to a raw hydrogen delivery line, and each section of the hydrogen compressor compression section comprises a hydrogen compressor compression cylinder 11 / 21 / 31 / 41, a cooler 18 / 28 / 38 / 48 and a separator 12 / 22 / 32 / 42 connected in sequence according to the flow direction of hydrogen, wherein the hydrogen compressor compression cylinder 11 of the first section is connected to the hydrogen compressor inlet separator 1, and the separator 42 of the last section is connected to the high-pressure hydrogenation reactor 3 via a pipeline;

[0063] The treatment system further includes a condensate flash tank 2, and the discharge pipelines 101 / 102 / 103 / 104 of each separator section are connected to the condensate flash tank 2, and each discharge pipeline is provided with a venturi nozzle 13 / 23 / 33 / 43.

[0064] A full-bore switch valve 14 / 24 / 34 / 44 is installed on the discharge pipeline 101 / 102 / 103 / 104 of each section, downstream of the Venturi nozzle 13 / 23 / 33 / 43. Its diameter matches the Venturi nozzle outlet on the same discharge pipeline. The full-bore switch valve 14 / 24 / 34 / 44 is controlled to open and close by the separator liquid level interlock system within this section.

[0065] The separator liquid level interlocking system of each section includes a liquid level monitor 16 / 26 / 36 / 46 installed on the separator 12 / 22 / 32 / 42, and a controller 17 / 27 / 37 / 47 connected to the liquid level monitor 16 / 26 / 36 / 46 and the full-bore switch valve 14 / 24 / 34 / 44 respectively; the interlocking threshold is set at 20% to 80% of the liquid level.

[0066] A replaceable anti-scour orifice plate 15 / 25 / 35 / 45 is installed on the drainage pipeline 101 / 102 / 103 / 104 of each work section, downstream of the full-bore switch valve 14 / 24 / 34 / 44, and the outlet pipeline of the anti-scour orifice plate 15 / 25 / 35 / 45 is connected to the condensate flash tank 2; the replaceable anti-scour orifice plate 15 / 25 / 35 / 45 adopts an eccentric porous array structure; the pore size is gradiently distributed, and the open porosity is ≤20%.

[0067] The disposal system of this embodiment also includes a circulating gas treatment section, which includes a circulating gas separator 52 and a circulating gas compressor 51; the gas outlet of the high-pressure hydrogenation reactor 3 is connected to the circulating gas separator 52 via a pipeline, the gas outlet of the circulating gas separator 52 is connected to the circulating gas compressor 51 via a pipeline, and the gas outlet of the circulating gas compressor 51 is connected to the high-pressure hydrogenation reactor 3 via a pipeline; the circulating gas separator discharge pipeline 105 is connected to the condensate flash tank 2.

[0068] The circulating gas separator discharge line 105 is equipped with a Venturi nozzle 53, a full-bore on-off valve 54, and a replaceable anti-scour orifice plate 55, arranged in sequence according to the material flow direction. The full-bore on-off valve 54 has a diameter that matches the outlet of the Venturi nozzle 53, and its opening and closing are controlled by the circulating gas separator liquid level interlock system. The circulating gas separator liquid level interlock system includes a circulating gas separator liquid level monitor 56 installed on the circulating gas separator 52, and a circulating gas treatment section controller 57 connected to the circulating gas separator liquid level monitor 56 and the full-bore on-off valve 54, respectively. The interlock threshold is set at 20% to 80% of the liquid level. The outlet pipeline of the anti-scour orifice plate 55 is connected to the flash tank 2 through the condensate main pipe 100. The anti-scour orifice plate 55 adopts an eccentric multi-porous array structure with a gradient pore size distribution and an open porosity of ≤20%.

[0069] The gas phase pipeline on the top of the condensate flash tank 2 is connected to the separator 1 at the inlet of the hydrogen compressor; a liquid level control valve is set at the bottom of the condensate flash tank 2 to discharge the condensate after analysis into the atmospheric pressure condensate tank 4, and finally sent to the sewage treatment system through the pump 5.

[0070] The discharge pipeline of the hydrogen compressor inlet separator 1 is connected to the atmospheric condensate tank 4.

[0071] This embodiment 5 provides a more preferred technical solution based on embodiment 4. Specifically: the gas phase pipeline on the top of the condensate flash tank 2 is connected to the separator 1 at the inlet of the hydrogen compressor; a liquid level control valve is set at the bottom of the condensate flash tank 2 to discharge the condensate after analysis into the atmospheric condensate tank 4, and finally sent to the sewage treatment system through the pump 5. The discharge pipeline of the separator 1 at the inlet of the hydrogen compressor is connected to the atmospheric condensate tank 4. This embodiment 5 connects the anti-scouring orifice plate outlet pipeline to the flash tank, and connects the tank top gas phase pipeline to the hydrogen compressor inlet raw hydrogen pipeline network, using 0.5~1.5kgf / cm 2 G low-pressure conditions achieve liquid hydrogen decomposition and recovery with a hydrogen recovery rate of ≥92%; a liquid level control valve is set at the bottom of the flash tank to discharge the condensate after decomposition with a dissolved hydrogen content of ≤5ppm into the atmospheric pressure condensate tank, and finally pumped into the sewage treatment system, significantly reducing the risk of explosion of hydrogen-containing wastewater.

[0072] This invention utilizes a unique drainage nozzle with a Churi-style structure, ensuring stable condensate discharge while effectively preventing gas leakage. A full-bore on-off valve is located downstream of the drainage nozzle. This valve is controlled by a separator level interlock, working together with the upstream drainage nozzle to safely control the separator's liquid level. A conveniently replaceable anti-scour plate is located downstream of the full-bore on-off valve. The anti-scour plate utilizes an eccentric, multi-hole design, mitigating scour from high-pressure liquid on the downstream piping while also throttling and reducing the pressure of the high-pressure liquid. Liquid from the outlet of each separator's condensate anti-scour plate is piped to a condensate flash tank. The gas phase pipeline at the top of the condensate flash tank connects to the raw hydrogen pipeline at the hydrogen compressor inlet. Dissolved hydrogen in the condensate is then desorbed and fed into the raw hydrogen pipeline. This effectively recovers the raw hydrogen while reducing the amount of dissolved hydrogen in the wastewater. Condensate collected in the condensate flash tank is discharged to an existing atmospheric condensate tank through liquid level control and then pumped to a wastewater treatment facility by a condensate pump. The amount of dissolved hydrogen in the condensate after low-pressure analysis is greatly reduced, which improves the operational safety of the sewage treatment plant.

[0073] The present invention uses a collaborative design of a full-bore switch valve and a replaceable anti-scour orifice plate to eliminate the erosion problem of the regulating valve and extend the comprehensive maintenance cycle to more than three times that of the original system. The present invention also uses a dual barrier of a Venturi nozzle + a full-bore switch valve to prevent accidental leakage of high-pressure hydrogen and reduce the risk of safety accidents by 95%. The system of the present invention can achieve efficient resource utilization: the hydrogen recovery rate is increased to 92% to 95%, and the annual hydrogen consumption cost is saved by approximately 1.5 million yuan (based on a production capacity of 100,000 tons / year). Using the system of the present invention, the dissolved hydrogen concentration in the sewage system is ≤5ppm, meeting the limit requirements of GB 31571-2015 "Petrochemical Industry Pollutant Emission Standard".

[0074] The above is only a preferred embodiment of the invention and does not impose any formal limitation on the invention. Based on the technical essence of the invention and within the spirit and principles of the invention, any simple modification, equivalent replacement and improvement of the above embodiment shall still fall within the scope of protection of the technical solution of the invention.

Claims

1. A system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of a 1,4-butanediol plant, comprising a hydrogen compressor inlet separator and a multi-stage hydrogen compressor compression section, characterized in that: The hydrogen compressor inlet separator is connected to the raw hydrogen delivery line. Each hydrogen compressor compression section includes a hydrogen compressor compression cylinder, a cooler and a separator connected in sequence according to the flow direction of hydrogen. The hydrogen compressor compression cylinder of the first section is connected to the hydrogen compressor inlet separator, and the separator of the last section is connected to the high-pressure hydrogenation reactor via a pipeline. The treatment system further includes a condensate flash tank, the discharge pipelines of each separator section are connected to the condensate flash tank, and each discharge pipeline is provided with a Venturi nozzle.

2. The system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of the 1,4-butanediol device according to claim 1, characterized in that: A full-bore switch valve is installed on the discharge pipeline of each section, downstream of the Venturi nozzle, and its diameter matches the outlet of the Venturi nozzle. The full-bore switch valve is controlled to open and close by the separator liquid level interlock system in this section.

3. The system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of the 1,4-butanediol device according to claim 2, characterized in that: The separator liquid level interlocking system of each section includes a liquid level monitor arranged on the separator, and a controller connected to the liquid level monitor and the full-bore switch valve respectively; preferably, the interlocking threshold is set at 20% to 80% of the liquid level.

4. A system for disposing liquid discharge from a compressor in a high-pressure hydrogenation process of a 1,4-butanediol plant according to any one of claims 1 to 3, characterized in that: A replaceable anti-scour orifice plate is provided on the drainage pipeline of each work section, downstream of the full-bore switch valve, and the outlet pipeline of the anti-scour orifice plate is connected to the flash tank; preferably, the replaceable anti-scour orifice plate adopts an eccentric porous array structure; more preferably, the pore size gradient distribution of the replaceable anti-scour orifice plate is ≤20%.

5. The system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of the 1,4-butanediol device according to claim 1, characterized in that: The process also includes a circulating gas treatment section, which includes a circulating gas separator and a circulating gas compressor; the gas outlet of the high-pressure hydrogenation reactor is connected to the circulating gas separator via a pipeline, the gas outlet of the circulating gas separator is connected to the circulating gas compressor via a pipeline, and the gas outlet of the circulating gas compressor is connected to the high-pressure hydrogenation reactor via a pipeline; the discharge pipeline of the circulating gas separator is connected to the condensate flash tank, and a Venturi nozzle is provided on the discharge pipeline of the circulating gas separator.

6. A system for disposing liquid discharge from a compressor in a high-pressure hydrogenation process of a 1,4-butanediol plant according to claim 5, characterized in that: A full-bore on-off valve is installed on the discharge line of the circulating gas separator, downstream of the Venturi nozzle. Its diameter matches the outlet of the Venturi nozzle. The full-bore on-off valve is controlled by the separator liquid level interlock system in this section. Preferably, the liquid level interlock system of the circulating gas separator includes a liquid level monitor provided on the circulating gas separator, and a controller connected to the liquid level monitor and the full-bore switch valve respectively; preferably, the interlock threshold is set to 20% to 80% of the liquid level; Preferably, a replaceable anti-scour orifice plate is provided on the discharge line of the circulating gas separator, downstream of the full-bore switch valve, and the outlet pipeline of the anti-scour orifice plate is connected to the flash tank; more preferably, the replaceable anti-scour orifice plate adopts an eccentric porous array structure; further preferably, the pore size gradient distribution of the replaceable anti-scour orifice plate has an opening rate of ≤20%.

7. The system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of the 1,4-butanediol plant according to claim 1, characterized in that: The gas phase pipeline on the top of the condensate flash tank is connected to the separator at the inlet of the hydrogen compressor; A liquid level joint control valve is installed at the bottom of the condensate flash tank to discharge the condensate after analysis into the atmospheric pressure condensate tank, and finally into the sewage treatment system through pumping.

8. The system for disposing the liquid discharge from the compressor of the high-pressure hydrogenation process of the 1,4-butanediol plant according to claim 1, characterized in that: The discharge pipeline of the hydrogen compressor inlet separator is connected to the atmospheric pressure condensate tank.

9. The system for disposing liquid discharge from the compressor of the high-pressure hydrogenation process of the 1,4-butanediol plant according to claim 1, characterized in that: The compression section of the multi-stage hydrogen compressor is four-stage.

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